Battery resetting process for scaffold fuel electrode

ABSTRACT

An electrochemical cell includes a fuel electrode configured to operate as an anode to oxidize a fuel when connected to a load. The cell also includes an oxidant electrode configured to operate as a cathode to reduce oxygen when connected to the load. The fuel electrode comprises a plurality of scaffolded electrode bodies. The present invention relates to an electrochemical cell system and method of resetting the electrochemical cell by applying a charge (i.e. voltage or current) to the cell to drive oxidation of the fuel, wherein the fuel electrode operates as an anode, and the second cell operates as a cathode, removing uneven distributions of fuel that may cause premature shorting of the electrode bodies to improve capacity, energy stored, and cell efficiency.

This application claims priority to U.S. Provisional Application Ser.No. 61/394,954, incorporated herein in its entirety by reference.

FIELD

The present invention is generally related to an electrochemical cell,and more particularly to a metal-air cell.

BACKGROUND

Electrochemical cells using metal as the fuel are known. A type ofelectrochemical cell is a metal-air cell, which typically comprises afuel anode at which metal fuel is oxidized, an air breathing cathode atwhich oxygen from ambient air is reduced, and an electrolyte forsupporting reactions of the oxidized/reduced ions.

In some metal-air cells, such as those disclosed in U.S. patentapplication Ser. Nos. 12/385,489 and 12/901,410, both of which areincorporated herein by reference, the fuel anode comprises a pluralityof scaffolded electrode bodies. Metal fuel is reduced andelectrodeposited on the electrode bodies. One challenge with this typeof design is ensuring that the growth does not prematurely shortadjacent electrode bodies together, thus cutting short the opportunityfor dense growth between the bodies.

In such scaffolded metal-air cells, manufacturing error, defects, andwear and tear of the air breathing cathode may result in some areas offuel on the electrode bodies not being oxidized as rapidly as otherareas when the cell is in a current generating mode. When such a cell isthen placed in a charging mode, these areas of built-up fuel may causepremature formation of electrical connections between the electrodebodies, which may reduce charge capacity, overall cell efficiency, andenergy stored in the battery.

Among other things, the present application endeavors to provide aneffective and improved way of eliminating the areas of metal fuel fromthe fuel anode, effectively resetting the fuel anode of the fuel cell toa fresh chargeable condition.

SUMMARY

According to an aspect of the present invention, there is provided amethod for resetting an electrochemical cell. The electrochemical cellincludes a fuel electrode, an oxidant electrode spaced from the fuelelectrode, a charging electrode selected from the group consisting of(a) the oxidant electrode, and (b) a third electrode spaced from thefuel and oxidant electrodes, and an ionically conductive mediumcontacting the electrodes. The fuel electrode and the oxidant electrodeare configured to, during discharge, oxidize a metal fuel at the fuelelectrode into a reducible fuel species and reduce an oxidant at theoxidant electrode to generate an electrical discharge currenttherebetween for application to a load. The fuel electrode and thecharging electrode are configured to, during re-charge, reduce thereducible species of the fuel to electrodeposit the fuel on the fuelelectrode and oxidize an oxidizable species of the oxidant byapplication of an electrical recharge current therebetween from a powersource. The method includes applying an electrical reset current betweenthe fuel electrode and at least one other aforesaid electrode of thecell with the fuel electrode functioning as an anode and the otheraforesaid electrode functioning as a cathode, such that the metal fuelon the fuel electrode is oxidized into the reducible fuel species. Byother aforesaid electrode, it is understood that if the chargingelectrode is the oxidant electrode, then the other aforesaid electrodeis the oxidant electrode. If the charging electrode is the thirdelectrode, however, then the other aforesaid electrode may be either theoxidant electrode or the third electrode. The method may also includeremoving the electrical reset current to discontinue the resettingprocess.

According to another aspect of the present invention there is providedan electrochemical cell system comprising an electrochemical cell and acontroller. The electrochemical cell contains a fuel electrode having aseries of permeable electrode bodies arranged in spaced apart relationfor receiving electrodeposited metal fuel. The cell also has an oxidantelectrode spaced apart from the fuel electrode, and a charging electrodespaced apart from the fuel electrode. The charging electrode is selectedfrom the group consisting of (a) the oxidant electrode, and (b) a thirdelectrode. The cell further contains an ionically conductive mediumcommunicating the electrodes. The electrochemical cell system may alsohave circuitry configured to provide electrical connections between thefuel electrode, the oxidant electrode, and the charging electrode. Thesystem may also contain a power input circuit and a power outputcircuit. There may also be a plurality of switches on the circuitry,configured to selectively open or close the electrical connections thebetween the fuel electrode, the oxidant electrode, the chargingelectrode, the power input circuit, and the power output circuit. In thecell system, the cell is configured to generate an electrical dischargecurrent by oxidizing the metal fuel on the electrode bodies of the fuelelectrode and reducing an oxidizer at the oxidant electrode. The spacedapart relation of the permeable electrode bodies of the fuel electrodemay enable an electrical recharge current to be applied between thecharging electrode and at least one of the permeable anode bodies, withthe charging electrode functioning as an anode, and the at least onepermeable electrode body functioning as a cathode. This configurationmay enable reducible fuel ions to be reduced and electrodeposited fromthe ionically conductive medium as fuel in oxidizable form on the atleast one permeable electrode body, whereby the electrodeposition causesgrowth of the fuel among the permeable electrode bodies, such that theelectrodeposited fuel establishes an electrical connection between thepermeable electrode bodies. The controller of the electrochemical cellsystem may be configured to control an open state or a closed state ofeach of the plurality of switches of the electrochemical cell inresponse to a control instruction. The controller may further beconfigured to selectively open and/or close the plurality of switches toapply an electrical reset current from a power source to the power inputcircuit, and between the fuel electrode and at least one other aforesaidelectrode, with the fuel electrode functioning as an anode and the otheraforesaid electrode functioning as a cathode, such that the metal fuelon the fuel electrode is oxidized into reducible fuel species. By otheraforesaid electrode, it is again understood that if the chargingelectrode is the oxidant electrode, then the other aforesaid electrodeis the oxidant electrode. If the charging electrode is the thirdelectrode, however, then the other aforesaid electrode may be either theoxidant electrode or the third electrode. The controller may also beconfigured to selectively open and/or close the plurality of switches toremove the electrical reset current to discontinue the resettingprocess.

Other aspects of the present invention will become apparent from thefollowing detailed description, the accompanying drawings, and theappended claims.

BRIEF DESCRIPTION OF THE DRAWINGS

Embodiments of the invention will now be described, by way of exampleonly, with reference to the accompanying schematic drawings in whichcorresponding reference symbols indicate corresponding parts, and inwhich:

FIG. 1 illustrates a cross-sectional view of an electrochemical cellsystem that includes two electrochemical cells;

FIG. 2 illustrates an exploded view of the electrochemical cell systemof FIG. 1;

FIG. 3 illustrates an electrode holder of one of the electrochemicalcells of FIG. 1;

FIG. 4 illustrates the electrode holder of FIG. 3 holding a fuelelectrode and a plurality of spacers connected to the electrode holder;

FIG. 5 illustrates one of the spacers of FIG. 4 in greater detail;

FIG. 6 illustrates a connection between the spacer of FIG. 5 and theelectrode holder of FIG. 3 in greater detail;

FIG. 7 illustrates a fluidization zone defined in part by the electrodeholder of FIG. 3 in greater detail;

FIG. 8 schematically illustrates electrical connections between theelectrochemical cell and an external load and a power supply accordingto an embodiment of the present invention

FIG. 9 schematically illustrates electrical connections between theelectrochemical cell and an external load and a power supply accordingto an embodiment of the present invention.

FIG. 10 is an isolated schematic view of the electrode bodies of anelectrochemical cell having a defect in an air cathode, showingelectrodeposited fuel growth thereon prior to the initial discharge ofthe cell;

FIG. 11 shows the consumption of the metal fuel of FIG. 10 duringdischarge;

FIG. 12 shows the continued consumption of the metal fuel of FIGS. 10and 11;

FIG. 13 shows the growth of the metal fuel of FIGS. 10-12 during therecharging of the electrochemical cell;

FIG. 14 shows the continued growth of the metal fuel of FIG. 13;

FIG. 15 shows the continued growth of the metal fuel of FIGS. 13 and 14;

FIG. 16 shows the consumption of the metal fuel of FIG. 15 duringdischarge;

FIG. 17 shows the cell of FIG. 16 in an effectively depleted state;

FIG. 18 shows the cell of FIG. 17 configured to be reset;

FIG. 19 shows an isolated schematic view of an electrochemical cellsystem comprising an electrochemical cell similar to that of FIG. 18,further comprising a controller; and

FIG. 20 shows a schematic view of an electrochemical cell systemcomprising a plurality of modules of the cells connected by acharge/discharge control system and a maintenance subsystem.

DETAILED DESCRIPTION

FIGS. 1 and 2 illustrate an electrochemical cell system 100 thatincludes two electrochemical cells 10 according to an embodiment of theinvention. As illustrated, each cell 10 includes a fuel electrode 12,and an oxidant electrode 14 that is spaced from the fuel electrode 12.The fuel electrode 12 supported by an electrode holder 16. Theelectrochemical system 100 also includes a cover 19 that is used tocover the electrochemical cells 10 on one side of the system 100, whileone of the electrode holders 16 is used to cover the opposite side ofthe system 100, as illustrated in FIG. 1.

In an embodiment, the fuel electrode 12 is a metal fuel electrode thatfunctions as an anode when the cell 10 operates in discharge, orelectricity generating, mode, as discussed in further detail below. Inan embodiment, the fuel electrode 12 may comprise a permeable electrodebody 12 a, such as a screen that is made of any formation able tocapture and retain, through electrodepositing, or otherwise, particlesor ions of metal fuel from an ionically conductive medium thatcirculates in the cell 10, as discussed in further detail below.

The fuel may be a metal, such as iron, zinc, aluminum, magnesium, orlithium. By metal, this term is meant to encompass all elements regardedas metals on the periodic table, including but not limited to alkalimetals, alkaline earth metals, lanthanides, actinides, and transitionmetals, either in atomic, molecular (including metal hydrides), or alloyform when collected on the electrode body. However, the presentinvention is not intended to be limited to any specific fuel, and othersmay be used. The fuel may be provided to the cell 10 as particlessuspended in the ionically conductive medium.

The ionically conductive medium may be an aqueous solution. Examples ofsuitable mediums include aqueous solutions comprising sulfuric acid,phosphoric acid, triflic acid, nitric acid, potassium hydroxide, sodiumhydroxide, sodium chloride, potassium nitrate, or lithium chloride. Themedium may also use a non-aqueous solvent or an ionic liquid. In thenon-limiting embodiment described herein, the medium is aqueouspotassium hydroxide.

The fuel may be oxidized at the fuel electrode 12 when the fuelelectrode 12 is operating as an anode, and an oxidizer, such as oxygen,may be reduced at the oxidant electrode 14 when the oxidant electrode 14is operating as a cathode, which is when the cell 10 is connected to aload and the cell 10 is in discharge or electricity generation mode, asdiscussed in further detail below. The reactions that occur duringdischarge mode may generate by-product precipitates, e.g., a reduciblefuel species, in the ionically conductive medium. For example, inembodiments where the fuel is zinc, zinc oxide may be generated as aby-product precipitate/reducible fuel species. The oxidized zinc orother metal may also be supported by, oxidized with or solvated in theelectrolyte solution, without forming a precipitate. During a rechargemode, which is discussed in further detail below, the by-productprecipitates, e.g., zinc oxide, may be reversibly reduced and depositedas the fuel, e.g., zinc, onto the fuel electrode 12, which functions asa cathode during recharge mode. During recharge mode, either the oxidantelectrode 14, or a separate charging electrode 70, described below,functions as the anode. The switching between discharge and rechargemodes is discussed in further detail below.

The electrode holder 16 defines a cavity 18 in which the fuel electrode12 is held. The electrode holder 16 also defines an inlet 20 and anoutlet 22 for the cell 10. The inlet 20 is configured to allow theionically conductive medium to enter the cell 10 and/or recirculatethrough the cell 10. The inlet 20 may be connected to the cavity 18 viaan inlet channel 24, and the outlet 22 may be connected to the cavity 18via an outlet channel 26. As illustrated in FIG. 3, the inlet channel 24and the outlet channel 26 may each provide a meandering tortuous paththrough which the ionically conductive medium may flow. The meanderingpath defined by the inlet channel 24 preferably does not include anysharp corners in which the flow of the medium may become stagnated or inwhich any particulates in the medium may collect. As discussed infurther detail below, the length of the channels 24, 26 may be designedto provide an increased ionic resistance between cells that are fluidlyconnected in series.

For each cell 10, a permeable seal member 17 may be bonded betweensealing surfaces on the electrode holders 16 and/or the cover 19, asappropriate, to enclose at least the fuel electrode 12 in the cavity 18.The seal member 17 also covers the inlet and outlet channels 24, 26. Theseal member 17 is non-conductive and electrochemically inert, and ispreferably designed to be permeable to the ionically conductive mediumin the orthogonal direction (i.e., through its thickness), withoutpermitting lateral transport of the ionically conductive medium. Thisenables the ionically conductive medium to permeate through the sealmember 17 for enabling ion conductivity with the oxidant electrode 14 onthe opposing side to support the electrochemical reactions, without“wicking” the ionically conductive medium laterally outwardly from thecell 10. A few non-limiting examples of a suitable material for the sealmember 17 are EPDM and TEFLON®.

In the illustrated embodiment, the cavity 18 has a generallyrectangular, or square, cross-section that substantially matches theshape of the fuel electrode 12. One side of the cavity 18, specifically,the side of the cavity 18 that is connected to the inlet channel 24,includes a plurality of fluidization zones 28 that are each connected tothe inlet channel 24 via a manifold that includes a plurality of cavityinlets 34 so that when the ionically conductive medium and precipitatesor reducible fuel species enter the cavity 18, the ionically conductivemedium and fuel enter the fluidization zones 28. As shown in greaterdetail in FIG. 7, each fluidization zone 28 is partially defined by twosurfaces 30, 32 that are angled with respect to each other but do nottouch each other so as to define diverging surfaces with respect to anaxis that extends from the inlet 34 through the center of thefluidization zone 28. In the illustrated embodiment, the surfaces 30, 32substantially define a “V” with an open bottom that is open to the inlet34, as illustrated in FIG. 3. Although the illustrated embodiment showsthe surfaces 30, 32 as being relatively straight, the surfaces may becurved or partially curved, so long as the surfaces 30, 32 are divergingfrom the inlet 34.

The fluidization zones 28 are configured so that as the ionicallyconductive medium with particulates flows into the cavity 18 via theinlet channel 24, the particulates are fluidized in the ionicallyconductive medium, which allows for the particulates to be more evenlydispersed in the ionically conductive medium as the ionically conductivemedium contacts the fuel electrode 12. This is particularly advantageouswhen the electrochemical cell 10 is oriented with the open bottom of theV-shaped fluidization zones 28 is pointed downward, as illustrated inFIG. 7. This is because gravity will tend to cause the particulates toaccumulate at the inlet end of the cavity 18 between the inlet channel24 and the outlet channel 26. By fluidizing the particulates in theionically conductive medium, and by providing a pressure drop across thecavity 18, as discussed in further detail below, the particulates willflow more evenly across the cavity 18, with substantially less or noaccumulation at the inlet end of the cavity 18. This may improve theefficiency of the cell 10 by providing a more even distribution of theparticulates across the surface of the fuel electrode 12.

As illustrated in FIG. 4, a plurality of spacers 40, each of whichextends across the fuel electrode 12 in a spaced relation to each other,are connected to the electrode holder 16 so that the fuel electrode 12may be held in place relative to the electrode holder 16 and to theoxidant electrode 14. In an embodiment, the fuel electrode 12 maycontain a plurality of permeable electrode bodies 12 a-12 c, asillustrated in FIG. 2, which may be separated by sets of the pluralityof spacers 40, so that each set of spacers 40 is positioned in betweenadjacent electrode bodies to electrically isolate the electrode bodies12 a-12 c from each other. Within each set of spacers 40 betweenadjacent electrode bodies, the spacers 40 are positioned in a spacedrelation in a manner that creates so-called “flow lanes” 42therebetween, as discussed in greater detail below. The flow lanes 42are three-dimensional and have a height that is substantially equal tothe height of the spacers 40. In an embodiment, the spacers may beprovided by a single frame that has cut-outs corresponding to the flowlanes. In an embodiment, the flow lanes may include a foam orhoneycomb-type structure that is configured to allow the ionicallyconductive medium to flow therethrough. In an embodiment, the flow lanesmay include an array of pins that are configured to disrupt the flow ofthe ionically conductive medium through the flow lanes. The illustratedembodiment is not intended to by limiting in any way.

The spacers 40 are non-conductive and electrochemically inert so theyare inactive with regard to the electrochemical reactions in the cell10. The spacers 40 are preferably sized so that when they are connectedto the electrode holder 16, the spacers 40 are in tension, which allowsthe spacers 40 to press against the fuel electrode 12, or one of theelectrode bodies 12 a-12 c, so as to hold the fuel electrode 12 orbodies thereof in a flat relation relative to the electrode holder 16.The spacers 40 may be made from a plastic material, such aspolypropylene, polyethylene, noryl, fluoropolymer, etc. that allows thespacers 40 to be connected to the electrode holder 16 in tension.

In the embodiment illustrated in FIG. 5, each spacer has an elongatedmiddle portion 44, and a shaped connecting portion 46 at each end. Theshaped connecting portions 46 are configured to be held by openings 48having substantially similar shapes in the electrode holder 16, asillustrated in FIG. 6. In the illustrated embodiment, the shapedportions 46 and the openings 48 have a substantially triangular shape,although the illustrated shape is not intended to be limiting in anyway. The substantially triangular shape provides surfaces 50 on oppositesides of the elongated portion 44 of the spacer 40 that are configuredto contact corresponding surfaces 52 on the electrode holder 16. Becausethe surfaces 50, 52 are angled with respect to a major axis MA of theelongated portion 44 of the spacer 40 and the tension in the spacer 40will be along the major axis MA, the forces created by the tension maybe distributed across a larger surface, as compared to a shaped portionhaving a circular or square shape with the same area.

Once the spacers 40 have been connected to the electrode holder 16 viathe end portions 46, the flow lanes 42 are defined across the cavity 18of the electrode holder 16. The spacers 40 are configured to essentiallyseal off one flow lane 42 a from an adjacent flow lane 42 b, that isseparated by one of the spacers 40 so that the ionically conductivemedium is guided to generally flow in substantially one direction.Specifically, the ionically conductive medium may generally flow in afuel direction FD across the fuel electrode 12, from the inlet channel24 to the outlet channel 26. A suitable pressure drop is generatedbetween the inlet channel 24 and the fluidization zones 28 so that theionically conductive medium may flow across the cavity 18 and to theoutlet channel 26, even when the cell 10 is oriented such that the flowis substantially upward and against gravity. In an embodiment, theionically conductive medium may also permeate through the fuel electrode12, or an individual permeable electrode body 12 a-12 c, in a seconddirection SD and into a flow lane that is on the opposite side of thefuel electrode 12 or permeable electrode body 12 a-12 c.

As illustrated in FIG. 8, the fuel electrode 12 is connected to anexternal load L so that electrons given off by the fuel as the fuel isoxidized at the fuel electrode 12 flow to the external load L. Theexternal load L may be coupled to each of the permeable electrode bodies12 a-12 c in parallel, as described in detail in U.S. patent applicationSer. No. 12/385,489, filed on Apr. 9, 2009 and incorporated herein byreference.

The oxidant electrode 14 functions as a cathode when the oxidantelectrode 14 is connected to the external load L and the cell 10operates in discharge mode. When functioning as a cathode, the oxidantelectrode 14 is configured to receive electrons from the external load Land reduce an oxidizer that contacts the second electrode 14. In anembodiment, the oxidant electrode 14 comprises an air breathingelectrode and the oxidizer comprises oxygen in the surrounding air.

The oxidizer may be delivered to the oxidant electrode 14 by a passivetransport system. For example, where oxygen present in ambient air isthe oxidizer, simply exposing the oxidant electrode 14 to ambient airvia openings in the cell, such as the openings that are provided bygrooves 54 in the cover 19 and grooves 56 in the electrode holder 16provided in the center of the electrochemical cell system 100, may besufficient to allow diffusion/permeation of oxygen into the oxidantelectrode 14. Other suitable oxidizers may be used and embodimentsdescribed herein are not limited to the use of oxygen as the oxidizer. Aperipheral gasket 15 may be positioned between the periphery of theoxidant electrode 14 and the cover 19 or electrode holder 16, asappropriate, to prevent the ionically conductive medium from leakingaround the oxidant electrode 14 and into the area in the grooves 54, 56for air exposure.

In other embodiments, a pump, such as an air blower, may be used todeliver the oxidizer to the oxidant electrode 14 under pressure. Theoxidizer source may be a contained source of oxidizer. Likewise, whenthe oxidizer is oxygen from ambient air, the oxidizer source may bebroadly regarded as the delivery mechanism, whether it be passive oractive (e.g., pumps, blowers, etc.), by which the air is permitted toflow to the oxidant electrode 14. Thus, the term “oxidizer source” isintended to encompass both contained oxidizers and/or arrangements forpassively or actively delivering oxygen from ambient air to the oxidantelectrode 14.

Electricity that can be drawn by the external load L is generated whenthe oxidizer at the oxidant electrode 14 is reduced, while the fuel atthe fuel electrode 12 is oxidized to an oxidized form. The electricalpotential of the cell 10 is depleted once the fuel at the fuel electrode12 is entirely oxidized or oxidation is arrested due to passivation ofthe fuel electrode (as described in greater detail below). A switch 60may be positioned in between the oxidant electrode 14 and the load L sothat the oxidant electrode 14 may be connected and disconnected from theload L, as desired.

To limit or suppress hydrogen evolution at the fuel electrode 12 duringdischarge mode and during quiescent (open circuit) periods of time,salts may be added to retard such a reaction. Salts of stannous, lead,copper, mercury, indium, bismuth, or any other material having a highhydrogen overpotential may be used. In addition, salts of tartrate,phosphate, citrate, succinate, ammonium or other hydrogen evolutionsuppressing additives may be added. In an embodiment, metal fuel alloys,such as Al/Mg may be used to suppress hydrogen evolution.

After the fuel in the cell 10 has been entirely oxidized, or whenever itis desirable to regenerate the fuel within the cell 10 by reducing theoxidized fuel ions back to fuel, the fuel electrode 12 and the oxidantelectrode 14 may be decoupled from the external load L and coupled to apower supply PS with the use of suitable switches 62, as illustrated inFIG. 8. The power supply PS is configured to charge the cell 10 byapplying an electrical current between the fuel electrode 12 and theoxidant electrode 14 such that the reducible species of the fuel isreduced and electrodeposited onto the permeable electrode bodies 12 a-12c and the corresponding oxidation reaction takes place at the oxidantelectrode 14, which is typically oxidation of an oxidizable species toevolve oxygen, which may be off-gassed from the cell 10. As described indetail in U.S. patent application Ser. No. 12/385,489, filed on Apr. 9,2009 and incorporated herein by reference, as an option only one of thepermeable electrode bodies, such as 12 a, may be connected to the powersupply PS so that the fuel reduces onto the permeable electrode body andprogressively grows to and on the other permeable electrode bodies 12b-12 c, one by one. The switches 62 may control when the cell 10operates in discharge mode and in charge mode. Additional switches 64may isolate each of the permeable electrode bodies, so that one, some,or all of the permeable electrode bodies are connected or disconnectedto the remainder of the cell 10.

Any suitable control mechanism may be provided to control the action ofthe switches 60, 62, 64 between the open and closed positions. Forexample, a relay switch that is biased toward the open position may beused, with an inductive coil coupled to the power supply that causesclosure of the switch when charging begins. Further, a more complexswitch that allows for individual connection to the permeable electrodebodies 12 a-12 c could be used to provide the connection/disconnectionto and from the load, and to and from each other.

FIG. 9 shows an embodiment where a third electrode 70 is provided tofunction as the charging electrode, rather than the oxidant electrode14. As illustrated in FIG. 2, the third electrode 70 may be positionedbetween the fuel electrode 12 and the oxidant electrode 14, with aspacer 72 and the seal member 17 being positioned between the thirdelectrode 70 and the oxidant electrode 14. The spacer 72 isnon-conductive and has openings through which the ionically conductivemedium may flow.

In the embodiment described above with respect to FIG. 8, the oxidantelectrode 14 functions as the cathode during power generation/discharge,and as the anode during charging, as described above. In FIG. 9, theload is coupled in parallel to each of the permeable electrode bodies 12a-12 c of the fuel electrode 12, and also to the third electrode 70during recharge. During current generation, the fuel on the fuelelectrode 12 is oxidized, generating electrons that are conducted topower the load L and then conducted to the oxidant electrode 14 forreduction of the oxidizer (as discussed in more detail above).

It is also possible in any of the embodiments of the invention to applythe cathodic potential simultaneously to all the electrode bodies 12a-12 c of the fuel electrode 12, rather than to just one to producebody-by-body progressive growth. Progressive growth emanating from oneterminal is advantageous because it provides more density. Specifically,the growth in the previously connected electrode bodies continues aseach subsequent body is connected by the progressing growth. With allthe electrode bodies subject to the same potential, the growth will onlyoccur until a short occurs between the charging electrode, which is theoxidant electrode 14 in the embodiment of FIG. 8 and the third electrode70 in the embodiment of FIG. 9, and the electrode body proximate to it.Thus, it is possible to have a faster, but less dense, growth in thismanner, which may be amenable to certain re-charging needs.

The embodiments illustrated in FIGS. 8 and 9 should not be considered tobe limiting in any way and are provided as non-limiting examples of howthe cell 10 may be configured to be rechargeable. U.S. patentapplication Ser. No. 12/885,268, filed on Sep. 17, 2010, the entirecontent of which is incorporated herein by reference, describesembodiments of a rechargeable electrochemical cell system withcharge/discharge mode switching in the cells.

In addition, any of the embodiments of the switches described above(e.g., to enable the charge mode, and discharge mode) may also be usedwith a plurality of electrochemical cells having a dynamically changingoxygen evolving (i.e., charging) electrode/fuel electrode, such as theprogressive one described in U.S. patent application Ser. No.13/230,549, incorporated in its entirety herein by reference. Forexample, as described in U.S. patent application Ser. No. 13/230,549,each cell 10 may also have its own plurality of switches associated withthe electrode bodies to enable progressive fuel growth.

For example, in an embodiment, during charging, the charging electrodeof each cell 10 may be coupled to the fuel electrode 12 of thesubsequent cell 10. In an embodiment, during charging, a first electrodebody 12 a of the fuel electrode 12 may have a cathodic potential and therest of the electrode bodies and/or a separate charging electrode mayhave an anodic potential. In such an embodiment, during the progressivefuel growth of the fuel electrode 12, the fuel may grow on the firstelectrode body 12 a having the cathodic potential and cause a short withthe adjacent electrode body 12 b having the anodic potential. Theadjacent electrode body 12 b may then be disconnected from the source ofanodic potential such that through electrical connection, the adjacentelectrode body 12 b also has the cathodic potential. This process maycontinue with the rest of the electrode bodies until no further growthis possible (i.e., the cathodic potential has shorted to the lastelectrode body having an anodic potential or a separate chargingelectrode). A plurality of switches may be provided toconnect/disconnect the electrode bodies to one another and/or to sourcesof cathodic or anodic potential. Thus, in such embodiments havingprogressive fuel growth, the charging electrode may be a separatecharging electrode from the fuel electrode 12 or may be at least theadjacent electrode body of the fuel electrode 12, up to all the otherelectrode bodies, having an anodic potential. In other words, thecharging electrode may be a separate charging electrode, an electrodebody having an anodic potential located adjacent to the at least oneelectrode body having a cathodic potential, and/or a group of electrodebodies having an anodic potential located adjacent to the at least oneelectrode body having a cathodic potential.

Thus, the charging electrode, as that term is used in the broaderaspects of this application, need not necessarily be a static ordedicated electrode that only plays the anodic charging role (althoughit may be), and it may at times be a body or bodies within the fuelelectrode to which an anodic potential is applied. Hence, the termdynamic is used to refer to the fact that the physical element(s)functioning as the charging electrode and receiving an anodic potentialduring charging may vary.

During discharging, the oxidant electrode 14 of a cell 10 may beoperatively connected to the fuel electrode 12 of the subsequent cell 10and fuel consumption would be through the electrode bodies (wherein theelectrical connection between the electrode bodies are through fuelgrowth). If a cell 10 is not functioning properly or for other reasons,the cell 10 may also be bypassed using the bypass switching features, asdescribed in U.S. patent application Ser. No. 12/885,268.

Also, in some embodiments, the cells may be designed as “bi-cells.” Thatterm refers to a pair of air electrodes that are on opposing sides of afuel electrode. During discharge, the air electrodes are at generallythe same cathodic potential and the fuel electrode is at an anodicpotential. Typically, a pair of dedicated charging electrodes may bedisposed in the ionically conductive medium between the air electrodesand the fuel electrode. During charging, the charging electrodes are atgenerally the same anodic potential, and the fuel electrode is at acathodic potential (alternatively, the charging electrode maydynamically charge, as described above). Thus, the air electrodes mayshare a common terminal, and the fuel electrode has its own terminal,and the charging electrodes may also share a common terminal. As such,electrochemically speaking, such a bi-cell may be regarded as a singlecell (although within the bi-cell, certain aspects of the cell, such asbi-directional fuel growth, may cause a bi-cell to be considered as twocells for certain purposes; however, at a higher level for modedischarging and connection management, those aspects are less relevantand the bi-cell can be viewed as a single cell). In an embodiment, thepair of air electrodes may correspond to the oxidant electrode 14, thefuel electrode may correspond to the fuel electrode 12, and the pair ofcharging electrodes may correspond to the third electrode 70.

Returning to FIG. 4, after the ionically conductive medium has passedthrough the fuel electrode 12, the medium may flow into the outletchannel 26 that is connected to the outlets 36 of the cavity 18 of theelectrode holder 16 and the outlet 22. The outlet 22 may be connected tothe inlet 20 in embodiments where the medium is recirculated in the cell10, or to an inlet of an adjacent cell, as discussed in further detailbelow, when a plurality of cells 10 are fluidly connected in series. Inan embodiment, the outlet 22 may be connected to a vessel to collect themedium that has been used in the cell 10.

The cells 10 illustrated in FIGS. 1 and 2 may be fluidly connected inseries. Details of embodiments of cells that are connected in series areprovided in U.S. patent application Ser. No. 12/631,484, filed Dec. 4,2009 and incorporated herein by reference in its entirety. The outlet 22of a first cell 10 may be fluidly connected to the inlet 20 of a secondcell 10, and the outlet 22 of the second cell 10 may be connected to theinlet 20 of a third cell, and so on. Although the embodiment of FIGS. 1and 2 illustrates two cells 10, additional cells may be stacked andfluidly connected to the illustrated cells. Due to the meandering,tortuous paths that are created by the inlet channel 24 and the outletchannel 26, described above and illustrated in FIGS. 3 and 4, the lengthof the flow passageways for the medium via the channels 24, 26 isgreater than the distance between the fuel electrode 12 and the oxidantelectrode 14 in each of the cells 10. This creates an ionic resistancebetween the pair of fluidly connected cells that is greater than anionic resistance within an individual cell 10. This may reduce orminimize internal ionic resistance loss of the stack of cells 100, asdiscussed in U.S. patent application Ser. No. 12/631,484, filed Dec. 4,2009.

In operation, the fuel electrode 12, which already has metal fueldeposited thereon, is connected to the load L and the oxidant electrode14 is connected to the load L. The ionically conductive medium entersthe inlet 20 under positive pressure and flows through the inlet channel24, the inlets 34 of the cavity 18, and into the fluidization zones 28of the flow lanes 42. The ionically conductive medium flows across thepermeable electrode bodies 12 a-12 c in the flow lanes 42 defined by theelongated middle portions 22 of the spacers 40. The ionically conductivemedium may also permeate through the permeable electrode bodies 12 a-12c of the fuel electrode 12. The ionically conductive mediumsimultaneously contacts the fuel electrode 12 and the oxidant electrode14, thereby allowing the fuel to oxidize and conduct electrons to theload L, while the oxidizer is reduced at the oxidant electrode 14 viathe electrons that are conducted to the oxidant electrode 14 by the loadL. After the ionically conductive medium has passed through the flowlanes 42, the medium flows out of the cavity 18 via the outlets 36 ofthe cavity 18, through the outlet channel 24, and out the outlet 22 ofthe cell 10.

When the potential of the cell 10 has been depleted or when it isotherwise desirable to recharge the cell 10, the fuel electrode 12 isconnected to the negative terminal of the power supply PS and thecharging electrode, which is the oxidant electrode 14 in the embodimentillustrated in FIG. 8 and the third electrode 70 in the embodimentillustrated in FIG. 9, is connected to the positive terminal of thepower supply PS. In the charging or recharge mode, the fuel electrode 12becomes the cathode and the charging electrode 14, 70 becomes the anode.By providing electrons to the fuel electrode 12, fuel ions may reduceinto fuel and redeposit onto the permeable electrode bodies 12 a-12 cwhile the ionically conductive medium circulates through the cell 10 inthe same manner as described above with respect to the discharge mode.

The flow lanes 42 provide directionality and distribution of theionically conductive medium across the fuel electrode 12. Thefluidization zones 28 agitate the particulates and precipitates thathave been formed during discharge mode of the cell 10 within theionically conductive medium and prevent the particulates from settlingout of the medium at the bottom of the cavity, which allows theparticulates to flow with the ionically conductive medium across thefuel electrode 12. The flow lanes 42 may also prevent the particulatesfrom settling and/or covering the electrodes. When the cell 10 is incharging mode, the improved distribution of the particulates across thefuel electrode 12 allow for a more uniform deposition of the reducedfuel onto the fuel electrode 12, which improves the density of the fuelon the fuel electrode 12, and increases the capacity and energy densityof the cell 10, thereby enhancing the cycle-life of the cell 10. Inaddition, by having the ability to control the distribution of theprecipitates or reaction by-product during discharge, earlypassivation/deposition of the by-product on the fuel electrode 12 may beprevented. Passivation, which can comprise areas of fuel being coveredby an oxide, preventing consumption of the fuel therein during dischargeand/or further fuel growth thereon during charge, leads to lower fuelutilization and lower cycle life, which is undesirable.

It may be appreciated that the electrochemical cell system 100 depictedherein is merely exemplary, and in other embodiments the functions orcomponents of the electrochemical cells 10 or the electrochemical cellsystem 100 may vary. For example, in various embodiments, the ionicallyconductive medium may flow through multiple cells 10, or may circulatewithin a single cell 10. In some embodiments, the ionically conductivemedium might generally not flow in the cell 10. It may be appreciatedthat portions of the electrochemical cell system 100, such as but notlimited to one or more cells 10 therein, and/or the constituent portionsthereof, may vary across embodiments. For example, various portions ofeach electrochemical cell 10 or other components of the electrochemicalcell system 100 may be of any suitable structure or composition,including but not limited to being formed from plastic, metal, resin, orcombinations thereof. Accordingly each cell 10 may be assembled in anymanner, including being formed from a plurality of elements, beingintegrally molded, or so on. In various embodiments the cell(s) 10and/or the housing(s) thereof may include elements or arrangements fromU.S. Pat. No. 7,722,988 and/or one or more of U.S. patent applicationSer. Nos. 12/385,217, 12/385,489, 12/549,617, 12/631,484, 12/776,962,12/885,268, 13/028,496, 13/083,929, 13/167,930, 13/185,658, 13/230,549,and 61/414,579, each of which are incorporated herein in theirentireties by reference. As such, embodiments of the present inventionare not limited to the management of the reaction by-product that isgenerated during discharge mode, as described above, and reversiblyreduced and electrodeposited as the fuel during recharge. Rather,embodiments of the present invention can be used where the reduciblefuel species is different from the reaction by-product and is suppliedseparately.

In some metal-air fuel cells, including those of the type described,wherein there is at least an oxidant electrode and a scaffolded fuelelectrode, imperfections in the oxidant electrode may reduce cellefficiency. FIGS. 10-16 show isolated schematic views of the cell 10,illustrating the growth morphology throughout the stack of electrodebodies 12 a-12 c in an exaggerated format to better understand theeffect of such imperfections. Similar to FIG. 9, FIGS. 10-16 show anembodiment where a third electrode 70 is provided to function as thecharging electrode, rather than the oxidant electrode 14. As wasillustrated in the embodiment of FIG. 2, the third electrode 70 seen inthe embodiments in FIGS. 10-16 is positioned between the fuel electrode12 and the oxidant electrode 14. The third electrode 70 may have thespacer 72 and the seal member 17 being positioned between the thirdelectrode 70 and the oxidant electrode 14. Also seen in FIGS. 10-16 isan imperfection 110 on the oxidant electrode 14. The detaileddescription of FIGS. 10-16 below demonstrates some undesirable effectsof the imperfection 14 during the discharging and recharging of the cell10.

In FIG. 10, the cell 10 is in a charging mode, wherein the fuelelectrode 12 and the third electrode 70 are connected to a power supply.In this configuration, the fuel electrode 12 becomes the cathode, andthe charging electrode 70 becomes the anode. By providing electrons tothe fuel electrode 12, fuel ions may reduce into fuel and electrodepositonto the permeable electrode bodies 12 a-12 c as a fuel growth 120,while the ionically conductive medium circulates through the cell 10. Inthe illustrated embodiment of the scaffolded configuration of theelectrode bodies 12 a-c, when the fuel electrode 12 is initiallyconnected to the power supply, only electrode body 12 a is electricallyconnected to the power supply. Therefore only electrode body 12 ainitially has a cathodic potential applied to it. During charging, asfuel ions are reduced into fuel deposited on the permeable electrodebody 12 a as the fuel growth 120, electrical connections eventually formwith permeable electrode body 12 b, creating a cathodic potential onelectrode body 12 b, as was described above. The fuel growth 120 seen inFIG. 10 exemplifies the cell 10 during its initial charging, or after afull re-setting (as discussed below), prior to any initiation of adischarging mode. At the stage of charging seen, the fuel growth 120 haselectrically connected electrode bodies 12 a and 12 b through densegrowth. The fuel growth 120 started to accumulate on electrode body 12b, however has not yet accumulated sufficiently to form an electricalconnection with electrode body 12 c.

Turning now to FIGS. 11 and 12, the cell 10 is in a discharge orelectricity generation mode. When the cell 10 is connected to a load, aswas described above, the fuel may be oxidized at the fuel electrode 12,with the fuel electrode 12 operating as an anode, and an oxidizer (i.e.oxygen) may be reduced at the oxidant electrode 14, with the oxidantelectrode 14 operating as a cathode. Due to the imperfection 110 of theoxidant electrode 14, oxidation of the fuel growth 120 may not begenerally uniform, as may be the case with a hypothetical ideal cell 10.Instead, as seen in FIG. 11, the imperfection 110 may cause an area ofunder-oxidation 130, wherein the fuel growth 120 has not been oxidizedinto the ionically conductive medium to the same extent as insurrounding areas. In some cases, the location of the area ofunder-oxidation 130 on the electrode bodies 12 a-c may correspond to thelocation of the imperfection 110 on the oxidant electrode 14.

Some areas of under-oxidation 130 may remain on the electrode bodies 12a-c even after the oxidation of fuel has caused there to no longer be anelectrical connection between the electrode bodies 12 a-c. An example ofthis may be seen in FIG. 12, where an area of under-oxidation 130remains on electrode body 12 b even though electrode body 12 b is nolonger electrically connected to electrode body 12 a. In the illustratedembodiment, because there is no electrical connection between electrodebodies 12 a and 12 b, there is no further oxidation of the metal fuel inthe area of under-oxidation 130 on electrode body 12 b. One effect ofthis residual area of under-oxidation 130 on the unconnected electrodebody 12 b of the illustrated embodiment can be reduced capacity of thecell 10, resulting from the unutilized potential of the fuel in the areaof under-oxidation 130. Depending on factors such as the nature of theimperfection 110, or for other reasons, such as passivation, some areasof under-oxidation 130 might not be oxidized and participate inelectricity generation, even when the electrode body (i.e. electrodebody 12 b) remains connected to the load. For example, passivation canlead to some or all of the area of under-oxidation 130 being covered byan oxide, preventing further oxidation even when the electrode bodyremains connected to the load. Again, such passivation of fuel can alsooccur on other areas of electrode bodies 12 a-c, not associated withimperfection 110 creating localized or broader areas that might not beoxidized and participate in electricity generation, and may prevent fuelgrowth thereon during subsequent charging.

FIGS. 13-16 show that such areas of under-oxidation 130 may also reducethe capacity of the cell 10 when the cell 10 is placed in a chargingmode while areas of under-oxidation 130 exist on the electrode bodies 12a-c. FIG. 13, for example, shows the cell 10 returned from theelectricity generating mode of FIG. 12 to a charging mode, wherein thefuel electrode 12 and the third electrode 70 are reconnected to thepower supply. As seen, the fuel growth 120 builds on and generallyfollows the contours of electrode body 12 a, including on the unconsumedfuel growth 120 existing thereon, such as the area of under-oxidation130. Although shown in exaggerated form in FIG. 13, it can be seen thatan electrical connection may form between electrode body 12 a andelectrode body 12 b at the area of under-oxidation 130 prior to anywhereelse between the electrode bodies 12 a-b. Once this electricalconnection is formed, and a cathodic potential is applied to electrodebody 12 b, fuel growth 120 accumulates on electrode body 12 b. In someembodiments, once this electrical connection forms, the fuel growth onprior electrode bodies, such as electrode body 12 a, may be reduced dueto initiation of growth on the newly connected body, preventing densegrowth throughout the stack of permeable electrode bodies 12 a-b, thusreducing overall capacity and cell efficiency.

As seen in the transition from FIG. 13 to FIG. 14, the fuel growth 120on electrode body 12 b may generally follow the contours of the surfaceof the electrode body 12 b, including on the area of under-oxidation 130remaining on electrode body 12 b from the prior discharge of the cell 10seen in FIGS. 11 and 12. The continued accumulation of fuel growth 120,including on the area of under-oxidation 130 on the electrode body 12 b,eventually may form an electrical connection with electrode body 12 c.Again this electrical connection may occur in the area ofunder-oxidation 130 prior to anywhere else between electrode bodies 12 band 12 c.

Because the initial charging of the cell 10 seen in FIG. 10 did notaccumulate fuel growth 120 on electrode body 12 c, there was no area ofunder-oxidation 130 on electrode body 12 c remaining from the initialdischarge utilizing the oxidant electrode 14 with the imperfection 110.Therefore, as seen in FIG. 15, wherein the recharging of the cell 10 hasprogressed such that the fuel growth 120 is occurring for the first timeon electrode body 12 c, the fuel growth 120 there may again be generallyuniform. However, as FIG. 16 demonstrates, once the cell 10 is placedback into an electricity generating mode, a new area of under-oxidation130 may begin to form on electrode body 12 c as a result of theimperfection 110.

In summary, areas of under-oxidation 130 on the scaffold electrode body12 c cause non-uniform electrical field and current distribution, whichmay lead to non-uniform deposits and poor cycleability of the fuelelectrode 12. Also, the overpotential for fuel (i.e. zinc) deposition onthe conducting scaffold electrode body 12 c (i.e. formed from nickel orcopper) is higher than the overpotential for fuel deposition on fuelpresent in under-oxidized areas, which may further result in non-uniformfuel growth 130, which may lower the charge capacity and result in poorcycleability of the fuel electrode 12.

One can visualize the problem of non-uniform growth with anunder-oxidation area by envisioning a board with a coat of paint 3 mmthick, and drawing a circle around an area representing the area ofunder-oxidation 130. During “discharge,” all 3 mm of the paint isremoved from the area around the circle (which is analogous to the fuelbeing oxidized off the electrode body), but in the circled“under-oxidation” area only 2 mm of the paint's thickness is removed,leaving a 1 mm “deposit” of paint in the “under-oxidation” area. Duringrecharging, as the paint is reapplied in an even manner (which isanalogous to the fuel being deposited on the electrode body), the“under-oxidation” area within the circle will reach the 3 mm thickness,but the surrounding area will only have 2 mm of paint thickness. Usingthis analogy, it can be appreciated how the area of under-oxidation 130can bridge the gap between adjacent electrode bodies 12 a-c morequickly, leaving less fuel (or paint in the analogy) deposited aroundit. Of course, this analogy is exaggerated and in reality a defect maycause under-oxidation to differ by a very small percentage—but over anumber of cycles this small percentage can exacerbate and create thesame problem.

One aspect of the present invention is a method of forcing oxidation ofthe otherwise unoxidized metal fuel remaining in the area ofunder-oxidation 130, placing the cell 10 in a resetting mode to performa resetting process. The areas of under-oxidation 130 may result fromnon-uniform fuel growth, passivated fuel, or for any other reason. Suchforced oxidation of the metal fuel may eliminate the areas ofunder-oxidation 130, so as to prevent the formation of prematureelectrical connections between electrode bodies 12 a-c in the areas ofunder-oxidation 130 prior to the formation of electrical connectionselsewhere in the fuel electrode 12. By preventing such prematureelectrical connections, the efficiency of cell 10 may improve byallowing dense fuel growth 120 between the scaffolded electrode bodies12 a-c.

The forced oxidation of the metal fuel may also or alternativelyeliminate passivated fuel deposits, restoring the electrode bodies 12a-c to a zero state of charge. Such forced oxidation of passivatedregions of metal fuel, by a resetting process at potential and currentconditions corresponding to a transpassive region, may eliminate theareas of under-oxidation 130. Thus, the formation of prematureelectrical connections between electrode bodies 12 a-c in the areas ofunderoxidation 130 prior to the formation of electrical connectionselsewhere in the fuel electrode 12 may be prevented. By preventing suchpremature electrical connections, the efficiency and charge capacity ofcell 10 may improve by allowing dense fuel growth 120 between thescaffolded electrode bodies 12 a-c.

In some embodiments, the forced oxidation of the metal fuel may bedesirable as a routine or preventative maintenance procedure. In anembodiment, forcing oxidation of the metal fuel may be utilized so as toplace the cell 10 in a transpassive regime, reducing the potential forsome of the metal fuel to passivate. For example, as the metal fuel onthe electrode bodies 12 a-c is depleted, the voltage will begin to drop,and the current will begin to spike, through the cell 10. In a zinc-airbattery, zinc may be oxidized without passivation at potentials of 800mV or above using an external load or resistor circuit. By continuing todrain the cell 10 under these conditions, the cell 10 may enter apassivation regime, wherein passivation of the fuel becomes more likely.By applying a small current to force oxidation of the remaining fuel atthat time, discussed in greater detail below, the cell 10 may be in atranspassive regime, where the oxide on the metal fuel surface may beporous and the metal fuel under the oxide may continue oxidation.

During operation of the cell 10, a decision may be made as to whether areset of the cell 10 would benefit the charge capacity of cell 10. Insome embodiments, the resetting process may be repeated a plurality oftimes. A decision to perform the resetting process may be made based onany suitable consideration. For example, in an embodiment, the passageof any set interval of time may be used to trigger a resetting process.In an embodiment, a randomized interval of time may be utilized. In someembodiments, the decision to reset the cell 10 may be based on thepassage of an interval of time from when the cell 10 was known to be inan efficient state, such as prior to the first discharge of the cell, orsince the previous iteration of the resetting process. For example, insome embodiments the cell 10 may be reset every 500 hours of discharge,or after fifty charge-discharge cycles. In some embodiments the durationof the reset process may range from ten minutes to one hour. The presentinvention is not intended to be limited to the duration of the resetprocess or the interval between resets on the cell 10.

Another consideration that may be utilized to determine if the resettingprocess should be initiated on the electrochemical cell 10 may include ameasurement of the charge capacity of the electrochemical cell 10. If asensor were to be attached to the electrochemical cell 10, for example,to measure the charge capacity of the cell 10, the sensed present chargecapacity could be compared to a value taken at a previous time,preferably at a time when it is known that no area of under-oxidation130 exists on the electrode bodies 12 a-c (such as prior to the firstdischarge of the cell 10, or immediately following a previous resettingprocess). If, for example, the present charge capacity is less than theprevious charge capacity by a greater than threshold amount, it may bedetermined that a resetting process should be initiated. As anothernon-limiting example, a sensor to detect the presence of unoxidizedmetal fuel when the cell 10 is depleted of charge may also be used todetermine if the resetting process is needed. Again, a threshold amountof unoxidized metal fuel may be determined as permissible in the cell 10despite the charge depleted state. In an embodiment, it may bedetermined that the resetting process should be initiated if a detectedor computed charge capacity for the cell 10 is reduced to between 50-80%of a rated charge capacity.

In another embodiment, the resetting process may be initiated if thecharge capacity in a previous cycle is lower than a target value beforeall of the electrode bodies are electrically connected to each other,potentially indicating non-uniform growth 130 of electrodeposited fuel.Electrical connections between the electrode bodies may be detected by aresistance or voltage measurement circuit. The resetting process mayalso be initiated if the charge capacity of a cell in a stack consistingof cells connected in series is lower than the average charge capacityof the stack. The reset may be performed on the individual cells or anarray of cells through an electrical circuit comprising switches toconnect or disconnect cells to the power supply during the resetprocess. In another embodiment, reset current may be applied after anygiven partial or complete discharge of the cell.

In some embodiments, the decision to initiate the resetting process maybe made based upon a voltage or current measurement of the cell 10. Sucha measurement may be useful when the reset process is a routinemaintenance operation, to prevent the fuel from sufficiently depletingto place the cell in a passivation regime, or for any other reason. Forexample, in an embodiment, once the voltage of the cell reduces to athreshold amount, it may be determined that the resetting process shouldbe initiated. In an embodiment, when the cell 10 is supplying betweenapproximately 0.7 and 1 V under a load, the resetting process may beinitiated. Likewise, if the current begins to increase over the cell 10,then the resetting process may also be desired. In an embodiment, theresetting process would be desired if the current through the cell 10 ismeasured at between approximately 10-75 mA/cm².

If it is determined that a resetting process is to be initiated on theelectrochemical cell 10, then the method may continue. In someembodiments, the method may comprise flowing (or continuing to flow) theionically conductive medium through the cell 10, including in variousembodiments through the inlets 34 and into the flow lanes 42, or intothe fluidization zones 28. The method may also comprise applying anelectrical reset current from a power source between the fuel electrode12 and the oxidant electrode 14, such that the fuel electrode 12functions as an anode and the oxidant electrode 14 functions as acathode. In such an embodiment, oxygen is reduced at the oxidantelectrode 14, and any remaining fuel is oxidized at the fuel electrode12. In another embodiment, the method may comprise applying theelectrical reset current from a power source between the fuel electrode12 and the third electrode 70 (i.e. the charging electrode). In such anembodiment, water is reduced at the third electrode 70, and anyremaining fuel is oxidized at the fuel electrode 12. In an embodimentwherein the third electrode has a low hydrogen evolution potential, thewater reduction and hydrogen evolution reaction occurs preferably overthe fuel reduction/deposition reaction. In either embodiment, any fuelpassivated by its oxide can be removed by maintaining the potential inthe transpassive regime.

The application of the electrical reset current may be such that themetal fuel growth 120, and in particular the area of under-oxidation 130on the electrode bodies 12 a-c are oxidized into reducible fuel species,such as reducible fuel ions. The amount of electrical reset current maybe any suitable amount that may drive the electrochemical reaction thatmay oxidize the metal fuel on the electrode bodies 12 a-c. In anembodiment, the electrical reset current, averaged over the area of thetotal electrode, may correspond to approximately greater than 0 mA/cm²through 10 mA/cm², and preferably 1-2 mA/cm², for example, when themetal fuel is zinc, and the oxidizer from the reduction reaction withthe air at the oxidant electrode 14, or from the reduction reaction withwater at the third electrode 70.

Depending on the configuration of the cell 10, the electric current maybe applied to each, one, some, or all of the electrode bodies 12 a-c ofthe fuel electrode 12. For example, FIG. 17 illustrates the cell 10having progressed in the discharge mode from the partially dischargedcondition seen in FIG. 16 to a mostly discharged condition, wherein theareas of under-oxidation 130 are no longer providing sufficient poweroutput to supply the load. Since, as seen, electrode bodies 12 b and 12c are no longer electrically connected to electrode body 12 a, theresetting process may not be effective in oxidizing the area ofunder-oxidation 130 on those electrode bodies 12 b-c. In an embodiment,to ensure that such a configuration in the cell 10 oxidizes metal fuelon subsequent electrode bodies 12 b-c, the resetting process maycomprise connecting the fuel electrode bodies of the cell 10 externally,so that electrical connections are formed between the electrode bodies12 a-c, before applying electrical reset current to oxidize the metalfuel. In an embodiment, the cell 10 may comprise selectively closedelectrical connections between the electrode bodies 12 a-c, so that theareas of under-oxidation 130 may be oxidized on each, some, or all ofthe electrode bodies 12 a-c.

As seen in the non-limiting embodiment in FIG. 18, the switches 64 maybe utilized to selectively move between an open and a closed electricalconnection, permitting or preventing the electrical reset current to beapplied to each of the electrode bodies 12 a-c. The switches 64 may beof any suitable form. Additionally, as described above, any suitablecontrol mechanism may be provided to control the action of the switches64 between open and closed positions. For example, as seen in FIG. 19,the electrochemical cell 10 may be part of an electrochemical cellsystem 140, which may further comprise a controller 150. As discussed ingreater detail below, in some embodiments multiple cells 10 may be inthe electrochemical system 140. The controller 150 may be of anysuitable type or configuration, including but not limited to aprocessor, a computer, electronic circuitry, and so on. The controller150 may be configured to have embedded control instructions. In anembodiment, the controller 150 may comprise an input to receive controlinstructions. In an embodiment, the controller 150 may be configured toselectively control an open state or a closed state of each of theplurality of switches 64 in response to the control instructions. Forexample, depending on the control instructions, the configuration of theplurality of switches 64 may place the electrochemical cell system 140in the charging mode, the discharging mode, or the resetting mode. In anembodiment, the controller 150 may also control some of the plurality ofswitches 64 to control connections to a power input circuit (shown inFIG. 19 as the “Power Supply”) and a power output circuit (shown in FIG.19 as the “Load”). Such a configuration may be useful so that manualdisconnection and reconnection of such electrical connections are notnecessary when changing the mode of the electrochemical cell system 140.

The processor of the controller 150, which may or may not be comprisedwithin the electrochemical cell system 140, may be configured toimplement the resetting process based on any suitable consideration. Inan embodiment, the controller 150 may be configured to first determineif the resetting process is needed for the electrochemical cell 10. Sucha determination may be based on a number of conditions, including butnot limited to the charge capacity of the cell, the passage of a timeinterval, or the passage of a number of charge and/or discharge cycles.For example, determining if the resetting process is needed may comprisesensing a present charge capacity for the cell, and comparing thepresent charge capacity to an initial, previous, or threshold chargecapacity. If the present charge capacity if less than the initial,previous, or threshold charge capacity by a threshold amount, thecontroller 150 may be configured to determine that a resetting processis needed, and to implement the process. As another example, determiningif the resetting process is needed may comprise determining if apredetermined amount of elapsed time has occurred since the cell 10 waslast discharged or last reset. As another example, determining if theresetting process is needed may comprise determining if a predeterminedamount of elapsed time has occurred since the cell 10 was lastdischarged or last reset. In an embodiment, the predetermined amount oftime may contain a randomized time interval. As another example,determining if the resetting process is needed may comprise determiningif a predetermined number of charges and/or discharges have occurredsince the electrochemical cell was initially charged, or last reset. Inan embodiment, the predetermined number of charges and/or discharges maybe randomized.

Eventually, the resetting process may be determined to be complete, andthe electrical reset current may be removed from the fuel cell 10 todiscontinue the resetting process. The determination to discontinue theresetting process may be achieved by any suitable means. In embodimentshaving an electrochemical cell system 140 with a controller 150, thedetermination to discontinue the resetting process may be made throughthe controller 150. Such a determination may be made from any suitableconsideration. For example, in an embodiment the elapse of an intervalof time, such as one known to be sufficient to completely oxidize allbut a threshold amount of metal fuel in the cell 10, may be used todetermine the completion of the resetting process. In an embodiment, thelack of detection of presence of metal fuel above a threshold value mayalso be used to signal that the cell 10 has been reset. In anembodiment, a detection of the amount of reducible fuel species in theionically conductive medium above a threshold value may also be used. Inan embodiment, a measurement of charge capacity of the cell 10 may alsobe used. In one non-limiting example, the measurement of charge capacitymay be taken at a set time interval following the commencement of theresetting process, and may be compared to a measurement taken prior tothe start of the resetting process, including preferably a measurementtaken when the cell 10 is known to be operating with an ideal chargecapacity.

As noted above, in some embodiments multiple cells 10 may be assembledinto electrochemical cell system 140. As shown in FIG. 20, in anembodiment electrochemical cell system 140 contains N modules 160 thatare connected by a charge/discharge control system 170. Each module 160may contain one or more cells 10. The charge/discharge control system170 may include connections to and from the power supply (when the cellsystem 140 is in a charging mode), and the load (when the cell system140 is in a discharge mode). In an embodiment, the charge/dischargecontrol system 170 may include controller 150 and switches 64 associatedwith each module 160. In an embodiment each cell 10 may have its ownassociated switches 64, and may have its own controller 150, that may becontrolled by a master controller within the charge/discharge controlsystem 170. In an embodiment, the charge/discharge control system 170may connect each module 160 with one or more control lines 180, whichmay communicate with the controller 150 associated with each cell ormodule, or may communicate directly with the switches 64 for each cellor module. As shown, each module 160 may be electrically connected tothe charge/discharge control system 170 through module terminals 190.

As shown in the illustrated embodiment of FIG. 20, electrochemical cellsystem 140 may further contain a maintenance subsystem 200. In anembodiment, maintenance subsystem 200 may be electrically connected tothe modules 160 by maintenance terminals 210. In an embodiment,maintenance subsystem 200 may be connected to the charge/dischargecontrol system 170 by a maintenance bus 220, which may, for example,connect a controller 150 within the maintenance subsystem 200 to acontroller within the charge/discharge control system 170. In anembodiment, maintenance subsystem 200 may be connected to controllers150 or switches 64 within each module 160 directly, or may connect tothe controllers 150 or switches 64 within each module 160 through themaintenance bus 220, the charge/discharge control system 170, and thecontrol lines 180. In an embodiment, the maintenance subsystem 200 maycontain its own controller 150.

In an embodiment, sensors may be provided in one or more of the cells10, the modules 160, the charge/discharge control system 170, themaintenance subsystem 200, or any other portion of electrochemical cellsystem 140. The sensors may be configured to communicate withcontrollers 150, so as to provide information that may determine how tocontrol switches 64 associated with the modules 160, thecharge/discharge control system 170, and/or the maintenance subsystem200. In an embodiment, sensors may provide information based upon thecurrent, voltage, fuel growth status, charge capacity measurement, orany other indicia of the status or health of cells 10, modules 160and/or electrochemical cell system 140. In an embodiment, thecharge/discharge control system 170 and/or the maintenance subsystem 200may be configured to selectively isolate one or more of cells 10 withinmodules 160, or one or more modules 160, so as to perform maintenance onthe cells 10 and/or the modules 160. In an embodiment, switches 64 mayinclude one or more bypass switches to isolate the one or more cells 10and/or the one or more modules 160. In various embodiments, themaintenance subsystem 200 and/or the charge/discharge control system 170may be configured to isolate one or more cells 10 within each module160, or isolate one or more modules 160 within the electrochemical cellsystem 140.

As an example, in the illustrated embodiment, if it were determined thata reset procedure would be desirable on the 2^(nd) module 160, such asby measuring a voltage drop or a current spike on the 2^(nd) module 160,the charge/discharge control system 170 may electrically disconnectswitches 64 associated with module terminals 190 associated with the2^(nd) module 160, so that only the 1^(st) and 3^(rd) through Nthmodules 160 are connected to the power supply 160 during charging or theload during discharging. In an embodiment, the 2^(nd) module 160 maythen be connected to the maintenance subsystem 200 through maintenanceterminals 210. In an embodiment, the reset current may then be providedto the 2^(nd) module 160, to force oxidation of any remaining metal fuelon the 2^(nd) module 160, including, for example, passivated deposits,or areas of under-oxidation 130. In an embodiment, the reset current maybe provided by the power supply, by the maintenance terminals 210, viathe charge/discharge control system 170, the maintenance bus 220, andthe maintenance subsystem 200. In an embodiment, a separate power supplyassociated with the maintenance subsystem 200 may provide the resetcurrent. In an embodiment where, for example, the reset current is to beapplied to the 2^(nd) module 160, the reset current may be drawn ordiverted from the current generated by the other modules 160 (i.e. the1^(st) and 3^(rd)-N^(th) modules 160). In such an embodiment, the resetcurrent provided by the other modules 160 may be provided frommaintenance terminals 210 for the other modules 160, through themaintenance subsystem 200, and through the maintenance terminals 210 forthe modules 160 to which the reset current is to be applied. In othersuch embodiments, the reset current may be provided by the other modules160 from the module terminals 190, through the charge/discharge controlsystem 170, the maintenance bus 220 and the maintenance subsystem 200.

In some embodiments, the electrochemical cell system 140 may contain oneor more voltage regulators and/or one or more current regulators. Suchvoltage or current regulators may be part of each cell 10, each module160, the charge/discharge control system 170, or the maintenancesubsystem 200. In an embodiment the voltage regulator and/or the currentregulator may be configured to convert power from the power supply orfrom the other modules 160 so as to provide the reset current asdescribed above. In an embodiment, the current regulator may beconfigured such that the reset current is above 0 mA/cm2 throughapproximately 10 mA/cm2. The direction of the reset current is such thatthe fuel electrode is oxidized electrochemically. In an embodiment, thevoltage regulator may be configured such that the reset currentcorresponds to a reset voltage (the difference Vc−Va between the Vc ofthe oxidant electrode 14 and the voltage Va of the fuel electrode 12) ofabove approximately −1V and below approximately 1V. In an embodiment,the reset current may be applied to the cell 10 and/or the module 160while the voltage measured across the cell 10 and/or module 160 is belowapproximately 0.5 V/cell. In an embodiment, once the voltage across thecell 10 and/or module 160 falls below −0.5 V/cell (or another thresholdvoltage, depending on the materials), the regulation of the resetcurrent may switch to be based on voltage. Such a switch at thethreshold voltage may be useful to keep the voltage so that oxidation ofthe metal fuel in the cell 10 and/or module 160 remains in thetranspassive regime. In some embodiments the reset current may beapplied for a set duration of time. In some embodiments, the currentsupplied by the cell 10 and/or the module 160 may be monitored, and thereset current may be discontinued once the current supplied by the cell10 and/or the module 160 drops below a threshold amount, indicating thatthe metal fuel has been consumed.

In some embodiments, the reset process may be preceded by the oxidationof fuel in the cell 10 under controlled voltage or current conditions,such as by using an electronic circuit containing a variable load toremove most of the fuel present on the fuel electrode 12. The voltage orcurrent may be selected such that no passivation of fuel occurs. Forexample, the cell 10 may be discharged at a fixed potential ofapproximately 1V. The transition to implementing the reset process maybe triggered based on a lower threshold limit for the current, forexample approximately 0.2 A flowing through the load. In an embodimenthaving constant voltage, the discharge voltage may range fromapproximately 0.7-1.1V (the difference between voltage of the oxidantelectrode 14 and the fuel electrode 12), and the current limit fortransition to reset process may range from approximately 0.25 mA/cm2 toapproximately 5 mA/cm2. In the case of constant current, the dischargecurrent may range from approximately 0.25 mA/cm2 to approximately 5mA/cm2 and the voltage limit for transition to reset process may rangefrom approximately 0.65V-1.1V. Optionally in an embodiment, all of thefuel electrode bodies 12 a-c may be externally connected through aswitch, as described earlier.

Where electrodes are referred to herein, it should be understood thatvarious structures in some embodiments may function as one or moreelectrodes in different ways depending on the operational mode of thedevice. For example, in some embodiments where the oxidant electrode isbi-functional as a charging electrode, the same electrode structure actsas an oxidant electrode during discharging and as a charging electrodeduring charging. Similarly, in the embodiment where the chargingelectrode is a dynamic charging electrode, all of the bodies of the fuelelectrode act as the fuel electrode during discharging; but duringcharging one or more of the bodies act as the fuel electrode byreceiving electrodeposited fuel and one or more other of the bodies actas the charging electrode to evolve the oxidant (e.g., oxygen), and thefuel electrode grows as the electrodeposited growth connects to more ofthe bodies. Thus, reference to an electrode is expressly defined aseither a distinct electrode structure or the functional role a structurecapable of multiple electrode functions may play during differentoperational modes of the cell (and thus the same multi-functionalstructure may be considered to satisfy multiple electrodes for thisreason).

The foregoing illustrated embodiments have been provided solely forillustrating the structural and functional principles of the presentinvention and are not intended to be limiting. For example, the presentinvention may be practiced using different fuels, different oxidizers,different electrolytes, and/or different overall structuralconfiguration or materials. Thus, the present invention is intended toencompass all modifications, substitutions, alterations, and equivalentswithin the spirit and scope of the following appended claims.

1. A method for resetting an electrochemical cell, the electrochemicalcell comprising: a fuel electrode comprising a series of permeableelectrode bodies arranged in spaced apart relation for receivingelectrodeposited metal fuel; an oxidant electrode spaced from the fuelelectrode; a charging electrode; an ionically conductive mediumcontacting the electrodes; the fuel electrode and the oxidant electrodebeing configured to, during discharge, oxidize the metal fuel at thefuel electrode and reduce an oxidant at the oxidant electrode togenerate a electrical discharge current therebetween for application toa load; and the fuel electrode and the charging electrode beingconfigured to, during re-charge, reduce a reducible species of the fuelto electrodeposit the fuel on the fuel electrode and oxidize anoxidizable species of the oxidant by application of a electricalrecharge current therebetween from a power source; the methodcomprising: applying an electrical reset current between the fuelelectrode and at least one other aforesaid electrode of the cell withthe fuel electrode functioning as an anode and the other aforesaidelectrode functioning as a cathode, such that the metal fuel on the fuelelectrode is oxidized into the reducible fuel species; and removing theelectrical reset current to discontinue the resetting process.
 2. Themethod of claim 1, wherein the electrical reset current between the fuelelectrode and the other aforesaid electrode provides approximately apotential difference capable of oxidizing a metal fuel on the fuelelectrode, and reducing an oxidant at the other aforesaid electrode. 3.The method of claim 1, further comprising repeating the method aplurality of times.
 4. The method of claim 1, further comprisingdetermining if a resetting process is needed for the electrochemicalcell, prior to applying the electrical reset current from the powersource.
 5. The method of claim 4, wherein determining if the resettingprocess is needed for the electrochemical cell comprises: sensing apresent charge capacity for the electrochemical cell; comparing thepresent charge capacity to an initial charge capacity; and if thepresent charge capacity is less than an initial charge capacity by agreater than a threshold amount, determining that a resetting process isneeded.
 6. The method of claim 4, wherein determining if the resettingprocess is needed comprises determining if a predetermined amount ofelapsed time has occurred since the electrochemical cell was lastdischarged, or since the electrochemical cell was last reset.
 7. Themethod of claim 6, wherein the predetermined amount of elapsed timecontains a randomized time interval.
 8. The method of claim 4 whereindetermining if the resetting process is needed for the electrochemicalcell comprises: sensing a present voltage between the permeableelectrode bodies; comparing the present voltage to an initial voltage;and if the present voltage is less than the initial voltage by greaterthan a threshold amount, determining that a resetting process is needed.9. The method of claim 4, wherein determining if the resetting processis needed for the electrochemical cell comprises: sensing a presentresistance between the permeable electrode bodies; comparing the presentresistance to an initial resistance; and if the present resistance isless than the initial resistance by greater than a threshold amount,determining that a resetting process is needed.
 10. The method of claim4, wherein determining if the resetting process is needed for theelectrochemical cell comprises: determining if the cell is entering apassivation regime where the metal fuel has an increased likelihood ofpassivating; and, if the cell is entering the passivation regime,applying the electrical reset current, wherein the electrical resetcurrent corresponds to oxidizing the metal fuel in a transpassiveregime, where the metal fuel has a decreased likelihood of passivating.11. The method of claim 10, further comprising, prior to applying theelectrical reset current, controlling the present voltage and/or theelectrical discharge current to consume a threshold amount of the fuelwithout entering the passivation regime.
 12. The method of claim 1,wherein the electrical reset current is approximately above 0 mA/cm2through 10 mA/cm2.
 13. The method of claim 1, wherein the electricalreset current corresponds to a reset voltage of above −1V through 1V.14. The method of claim 1, wherein the charging electrode is selectedfrom the group consisting of (a) the oxidant electrode, (b) a thirdelectrode spaced from the oxidant electrode, and (c) a portion of thefuel electrode.
 15. The method of claim 14, wherein the chargingelectrode during recharge is a dynamic charging electrode comprising atleast some of the permeable electrode bodies.
 16. The method of claim14, wherein the charging electrode is the oxidant electrode, and theother aforesaid electrode is thus also the oxidant electrode, andwherein the other aforesaid electrode reduces oxygen.
 17. The method ofclaim 14, wherein the charging electrode is the third electrode, and theother aforesaid electrode is the oxidant electrode, and wherein theother aforesaid electrode reduces oxygen.
 18. The method of claim 14,wherein the charging electrode is the third electrode, and the otheraforesaid electrode is also the third electrode, and wherein the otheraforesaid electrode reduces water in the ionically conductive medium.19. The method of claim 14, wherein the charging electrode is the thirdelectrode, and the other aforesaid electrode is also the thirdelectrode, and wherein the other aforesaid electrode reduces oxygendissolved within the ionically conductive medium.
 20. The method ofclaim 1, wherein the electrochemical cell further comprises an electrodeholder comprising a cavity for holding the fuel electrode, a pluralityof inlets connected to the cavity on one side of the cavity andconfigured to supply the ionically conductive medium to the cavity, anda plurality of outlets connected to the cavity on an opposite side ofthe cavity and configured to allow the ionically conductive medium toflow out of the cavity.
 21. The method of claim 20, wherein theelectrochemical cell further comprises a plurality of spacers extendingacross the fuel electrode and the cavity in a spaced relation from eachother to define a plurality of flow lanes in the cavity, wherein one ofthe plurality of inlets and one of the plurality of outlets areassociated with each flow lane so that the ionically conductive mediumflows into each flow lane via the associated inlet, across the fuelelectrode, and out of the flow lane via the associated outlet.
 22. Themethod of claim 21, further comprising flowing the ionically conductivemedium through the inlets and into the flow lanes, prior to applying theelectrical reset current from the power source.
 23. The method of claim1, wherein the electrochemical cell further comprises an electrodeholder comprising a cavity for holding the fuel electrode, and apassageway through which the ionically conductive medium flows into thecavity, wherein the cavity comprises a plurality of fluidization zones,each fluidization zone being at least partially defined by divergingsurfaces where the passageway is connected to the cavity, thefluidization zones being configured to fluidize precipitates in theionically conductive medium as the ionically conductive medium flowsinto the cavity.
 24. The method of claim 23, further comprising flowingthe ionically conductive medium into the fluidization zones prior toapplying the electrical reset current from the power source.
 25. Anelectrochemical cell system comprising: an electrochemical cellcomprising: a fuel electrode comprising a series of permeable electrodebodies arranged in spaced apart relation for receiving electrodepositedmetal fuel; an oxidant electrode spaced apart from the fuel electrode; acharging electrode; an ionically conductive medium communicating theelectrodes; circuitry configured to provide electrical connectionsbetween the electrodes, a power input circuit, and a power outputcircuit; a plurality of switches in the circuitry, configured toselectively open or close the electrical connections the between theelectrodes, the power input circuit, and the power output circuit;wherein the cell is configured to generate an electrical dischargecurrent by oxidizing the metal fuel on the electrode bodies of the fuelelectrode and reducing an oxidizer at the oxidant electrode; and whereinthe spaced apart relation of said permeable electrode bodies of the fuelelectrode enables an electrical recharge current to be applied betweenthe charging electrode and at least one of the permeable anode bodieswith the charging electrode functioning as an anode and the at least onepermeable electrode body functioning as a cathode, such that reduciblefuel ions are reduced and electrodeposited from the ionically conductivemedium as fuel in oxidizable form on the at least one permeableelectrode body, whereby the electrodeposition causes growth of the fuelamong the permeable electrode bodies such that the electrodeposited fuelestablishes an electrical connection between the permeable electrodebodies; and a controller configured to control an open state or a closedstate of each of the plurality of switches of the electrochemical cell,wherein the controller is further configured to initiate a resettingprocess by: selectively operating the plurality of switches to apply anelectrical reset current from a power source to the power input circuitand between the fuel electrode and at least one other aforesaidelectrode with the fuel electrode functioning as an anode and the otheraforesaid electrode functioning as a cathode, such that the metal fuelon the fuel electrode is oxidized into a reducible fuel species; andselectively operating the plurality of switches to remove the electricalreset current to discontinue the resetting process.
 26. Theelectrochemical cell system of claim 25, wherein the controller isconfigured to determine if the resetting process is needed for theelectrochemical cell, prior to applying an electrical reset current fromthe power source.
 27. The electrochemical cell system of claim 26,wherein determining if the resetting process is needed for theelectrochemical cell comprises: sensing a present charge capacity forthe electrochemical cell; comparing the present charge capacity to aninitial charge capacity; and if the present charge capacity is less thanan initial charge capacity by a greater than a threshold amount,determining that a resetting process is needed.
 28. The electrochemicalcell system of claim 26, wherein determining if the resetting process isneeded comprises determining if a predetermined amount of elapsed timehas occurred since the electrochemical cell was last discharged, orsince the electrochemical cell was last reset.
 29. The electrochemicalcell system of claim 28, wherein the predetermined amount of elapsedtime contains a randomized time interval.
 30. The electrochemical cellsystem of claim 26, wherein determining if the resetting process isneeded comprises determining if a predetermined number of discharge andrecharge cycles have occurred since the electrochemical cell wasinitially charged or last reset.
 31. The electrochemical cell system ofclaim 26, wherein determining if the resetting process is neededcomprises determining if a randomized number of discharge and rechargecycles have occurred since the electrochemical cell was initiallycharged or last reset.
 32. The electrochemical cell system of claim 26,wherein determining if the resetting process is needed for theelectrochemical cell comprises: sensing a present voltage between thepermeable electrode bodies; comparing the present voltage to an initialvoltage; and if the present voltage is less than the initial voltage bygreater than a threshold amount, determining that a resetting process isneeded.
 33. The electrochemical cell system of claim 26, whereindetermining if the resetting process is needed for the electrochemicalcell comprises: sensing a present resistance between the permeableelectrode bodies; comparing the present resistance to an initialresistance; and if the present resistance is less than the initialresistance by greater than a threshold amount, determining that aresetting process is needed.
 34. The electrochemical cell system ofclaim 26, wherein determining if the resetting process is needed for theelectrochemical cell comprises: determining if the cell is entering apassivation regime where the metal fuel has an increased likelihood ofpassivating; and, if the cell is entering the passivation regime,applying the electrical reset current, wherein the electrical resetcurrent corresponds to oxidizing the metal fuel in a transpassiveregime, where the metal fuel has a decreased likelihood of passivating.35. The electrochemical cell system of claim 25, wherein the electricalreset current is approximately above 0 mA/cm2 through 10 mA/cm2.
 36. Theelectrochemical cell system of claim 25, wherein the electrical resetcurrent corresponds to a reset voltage of above −1V through 1V.
 37. Theelectrochemical cell system of claim 25, wherein the charging electrodeis selected from the group consisting of (a) the oxidant electrode, (b)a third electrode spaced from the oxidant electrode, and (c) a portionof the fuel electrode.
 38. The electrochemical cell system of claim 37,wherein the charging electrode during re-charge is a dynamic chargingelectrode comprising at least some of the permeable electrode bodies.39. The electrochemical cell system of claim 37, wherein the chargingelectrode is the oxidant electrode, and the other aforesaid electrode isthus also the oxidant electrode, and wherein the other aforesaidelectrode reduces oxygen.
 40. The electrochemical cell system of claim37, wherein the charging electrode is the third electrode, and the otheraforesaid electrode is the oxidant electrode, and wherein the otheraforesaid electrode reduces oxygen.
 41. The electrochemical cell systemof claim 37, wherein the charging electrode is the third electrode, andthe other aforesaid electrode is also the third electrode, and whereinthe other aforesaid electrode reduces water in the ionically conductivemedium.
 42. The electrochemical cell system of claim 37, wherein thecharging electrode is the third electrode, and the other aforesaidelectrode is also the third electrode, and wherein the other aforesaidelectrode reduces oxygen dissolved within the ionically conductivemedium.
 43. The electrochemical cell system of claim 25, furthercomprising a plurality of the electrochemical cell and a secondplurality of switches therebetween, wherein the controller is furtherconfigured to selectively open and/or close the second plurality ofswitches to apply the electrical reset current from the power source tothe power input circuits of one or more of the plurality of theelectrochemical cell.
 44. The electrochemical cell system of claim 43,wherein the controller is further configured to determine if a resettingprocess is needed for each of the plurality of electrochemical cells,and if the resetting process is needed for at least some of theplurality of electrochemical cells, initiating the resetting process forthe at least some of the plurality of electrochemical cells.